Means for distributing solids in gases in catalytic apparatus



J. S. PALMER Feb. 19, 1952 MEANS FOR DISTRIBUTING SOLIDS IN GASES IN CATALYTIC APPARATUS Filed Feb. 14, 1948 AGENT.

Patented Feb. 19, 1952 MEANS FOR DIs'rRIBUTING soLms 1N GASES 1N oA'rALYTIo APPARATUS Jewell S. Palmer, -Wooster, Tex., assig'nor, by

mesne assignments, to Standard Oil Development Company, Elizabeth, N. J., a corporation A of Delaware Application February 14, 1948, Serial No. 8,336

3 claims. l

The present invention is directed to a method andl to apparatus for distributing solids in a gas; eous stream. More particularly, the invention is directed to a method and apparatus for allowing distribution of catalyst in a stream of free oxygen-containing gas, or other gasiform inaterial. f-

The invention also has to do with an apparatus and a method for distributing catalyst in a gaseous medium in a cracking operation in which a suspension of finely divided catalyst is formed in a hydrocarbon and the hydrocarbon cracked in said suspension. This type of catalytic cracking operation is known to the art as the'iluid flow type. There are two types of fluid catalytic cracking operations, the so-called downflow operation and the upflow method. In the downflowtype of fluid flow catalytic cracking there is provided a reactor and a regenerator. Finely divided catalyst, in suspension in vapors of the hydrocarbons to be cracked, is fed into the bottom of the reactor. The velocity of flow of the hydrocarbons is regulated so that hydrocarbon vapors carry the catalyst to an intermediate point in the reactor at which point there is a concentration ofvcatalyst resulting in the forming of a dense zone from the outer annulus of which the catalyst particles drop to the bottom of the reactor `from which they are withdrawn. Upon leaving the reactor the catalyst particles are picked up by a stream of..hot air which carries them to the regenerator where the carbonaceous materials deposited Von the catalyst in the reactor are consumed by combustion.v .The catalyst ow in the regenerator follows the same pattern as to the reactor with regenerated catalyst falling into a well inthe lower. `section of the regenerator from lwhich point it is fed back to the reactor. A detailed description of the downflow type of fluid Aiiow catalytic cracking process is given in U. S. Patent 2,407,374 to Conrad H Kollenberg.

Y In the upiioW type ofv iluid' oW catalytic crack-p ing, a reactor and a regenerator are also enig- A ployed.' Finally'divided catalyst, in suspension" the vreactor are burnedoff in thepresence of con#4 trlled amounts" -of air. Thecatalyst from the regeneratoiisA separated from the gaseous' prod- The catalyst is 2 ucts of combustion and is then fed back to the reactor.

It is well known to employ either of these two types of fluid flow cracking to convert relatively high molecular weight hydrocarbons, such as heavy naphtha or gas oil and the like, to relatively low molecular weight hydrocarbons, such as light naphtha, in the presence of powdered catalyst comprising oxides of silicon and aluminum, silicon and zirconium, or silicon and titanium, certain specially activated natural clays, and the like at temperatures in the range of about 850 to 1100" F. In these catalytic cracking operations in which hydrocarbons are cracked by the socalled uid flow technique, solid catalyst particles having diameters in the range from about 0 to mu with a predominating part in the range between 20 and 100 mu are suspended in the hydrocarbon to be cracked, passed to a reaction zone, and the reaction product separated from the catalyst. It is necessary to handle immense quantities of catalyst in View of the nature of the process. For example, in a reaction zone of a typical catalytic cracking operation of the fluid flow type, anywhere from about 20 to about 55 tons of catalyst per minute may be Withdrawn from a reaction zone of a unit charging as much as 25,000 to 35,000 barrels of feed stock per day. This amount of catalyst discharges from the reactor of a downlow unit into a line connecting the reactor and the regenerator including a regeneration zone in which combustion conditions are maintained to burn oi carbonaceous mate-A rial deposited on the catalyst. The vast amount of catalyst passing from the reactor into the lines connecting the reaction Zone to the regenerator zone frequently results in the buildup of catalyst in these lines. It might be mentioned that the enormous quantities of catalyst coupled with the tremendous iiow of vaporized hydrocarbon or' other gaseous material requires pipes orv conduits having diameters of anywhere from 6 to 9 feet. Thus, the immense amounts of catalyst dropping into these large lines frequently .build up in the lines and cause pressure dro-p which results in a lowering of the capacity of the whole unit. Under best operating conditions, of course, the catalyst dropping from a vertical conduit into a more or less horizontal conduit transverse the vertical conduit, is picked up by a blast of air or other gaseous material to be transported to the regeneration zone where combustion conditions are maintained.' However, this is not always the case, and as mentioned before, the catalyst may accumulate at a point adjacent the outlet from vto Fig. 1, numeral I I designates a reaction cham- Fig. 2 shows an arrangement of the apparatus arranged in a transverse conduit below a vertical conduit;

Fig. 3 shows a section of the conduit including the apparatus of the present invention taken along the line III-III of. Fig. 2.; and.

Fig. 4 is a view of the'. apparatus' of the present invention shown in perspective and withdrawn from and independent of the conduit.

Referringvnovv to the drawing and especially "'ber' and numeral I2 designates a regeneration cause distribution of catalyst particles as they drop down across the baille into a flow of agaseous fluid.

The objects of the present invention are achieved by locating in a transverse conduit adjacent a vertical conduit connecting yinto the transverse conduit, a vertical partition or center member across which baiiie plates depend at an angle greaterA than 90 and which are attached, both to the center member and to the walls of the conduit in which the structure is located.

Therefore, in accordance. with the present in. vention, buildup of catalyst in the large lines employed in catalytic cracking of the uid ow type is substantially reduced by providing a structure including apparatus elements which allow distribution of the catalyst in ythese large lines so that it may be easily picked up and carried by the gas which may be oxygen-containing gas or air, which is used to transport it., and which utlimately serves as a source oxygen in the regeneration operation.

The apparatus including. the preferred` structure of the present invention includes a device which may be positioned in a conduit transverse a vertical conduit from a reaction chamber of Ya fluid flow catalytic cracking operation to provide a baille arrangement for dispersion of catalyst in ly connected to the walls of the transverse con- .3

duit. The baiiies are arranged to provide a cascade effect of downowing catalyst through thevertical conduit from the reaction zone into. the.i transverse conduit and should `be arranged to form angles with the center partition member greater than 90.

In a typical arrangement of apparatus in accordance with the present invention,y in a conduit of 8 feet in diameter a partition is` centered in the transverse conduit from its dependent. baille structure members to provide a cascade acmss the conduit. A typical arrangement will include at least 5 baiiies on each side of acenter partition member arranged at an angle greater than a right angle but less than 180. The angle at which the baiiles are arranged, of course, will depend upon the nature of the solids being handled.

The present invention may be more clearly understood from the following detailed description. of the accompanying drawing in which.

Fig. 1 is a diagrammatic flow sheet of a downow catalytic cracking system employing the. feature of the present invention and showingA its relationto the reaction chamber. and the regeneration chamber;

chamber. Regenerator I2 is fluidly connected to reactor II- by conduit I3 and reactor II is uidly connected` to regenerator I2 by vertical conduit I4 and transverse conduit I5. Reactor II is provided with a separator I6 which may be one of the cyclone type although other separating meansV may be provided. Reactor II is also provided with an outlet line I1 by way of which product is removed therefrom. Regenerator I2 is also provided with a separator.` I8 which may be a cyclone separator similar to separator Isin reactor II. a line I9 which discharges into a Cottrell. precipitator 20 by way of which separation may be made between any ne catalyst particles leaving regenerator I2 by line I9. Cottrell precipitator 20 is .provided with a line or stack 2I through which combustion gases may be discharged therefrom and. with a line 22 to discharge separated catalyst particles back into the regenerator I2.

Hydrocarbon feed stock is introduced` into line I3 by line 23 and air for circulation of catalyst.

from reactor II to regenerator I2, and for. regeneration of the catalyst in regenerator I2 may be introduced byline 24.

Located in. conduit I5 at a point. immediately below cone member 25 is a bale structure 26 which is laid transverse thev conduit I5. This baille structure. 26 comprises a center. partition.

member 21 indicated by the dotted line and baille plates 28 29,. 30 3|, and 32.

In accordance` with the description taken. in conjunctionwith Fig. 1 of the drawing,Y a hydrocarbonfeed such as a gasoil hydrocarbon is irl-- troduced into the. system by way of. line 23 where it is met by a flow. of hot catalyst particles withdrawn. from regenerator I2 by funnel shaped member 33 in line I3. The suspension. of catalyst particles. in hydrocarbon feeds into. the. re, actor II through funnel shaped. member- 34 wherein a dense. phase of catalyst and hydrocarbons is maintained; reaction conditions are adjusted for catalytic cracking ofthe hydrocarbons. Asmentioned before, a temperaturev in the range between 850 and 1100,o F. will be maintained in reaction zone II.

In reactor I I, the.- catalytic cracking operation.

takes place withthe products and suspended catalyst flowing .upwardlyinto cyclone separator I6 wherein a, separation is made between the hydro.- carbons and the catalyst with. the. catalyst. dropping back into the reactor II and the productl withdrawn to a fractionation zone, not showmby line I1.. Thecatalyst drops back to the outer annulus of reactor I I .and thence downward into the.

Regenerator I2 is also provided with Ordinarily thev temperature. will be in the range from about 940 to about.

duit I5,l passing through cone shaped member 25 whichrestricts the ow and thereby'increasesthe velocity of the flow of catalyst prior to its entering the conduit I5. Prior tothe present invention, pressuredrop acrossthe conduit I5 was being `errperienced by buildup of catalyst immediately before and after the point indicated by the numeral 35. For some unknown reason the catalyst dropping down into-the conduit. I5 was not being adequately uidized by the air being introduced by line 24. 'Ille baffle members 28, 29, 30, 3l and 32 allow distribution of the catalyst across the ow of air and gives the air time to pick up the catalyst and adequately fluidize and carry it through the conduit I 5 and thence to the regen'- erator I2 where the regeneration reaction takes place by maintenance of combustion conditions therein.

Referring now to Fig. 2, identical numerals will be employed to identify similar parts with respect to Fig. 1. Numeral I4 designates a conduit through which catalyst flows from-a reaction zone to a conduit I5 and particularly through a cone shaped member 25 into the conduit I5. The conduit is connected to a third conduit 24 through which air is introduced to transport the catalyst falling into the conduit I5. The air flows in a direction indicated by the arrows and is introduced across the downflowing catalyst by conduit 24. Immediately ahead of and across the point of ingress and below conduit I4 is arranged a center member 21 provided with bailies 28, 29, 30, 3| and 32.

As will be seen, the baIles 28, 29, 30, 3l, and 32 are arranged at an angle with the center member 21 as shown in Fig. 3 to allow a cascade effect of the catalyst flowing down and across the baiile arrangement. This prevents buildup of catalyst in the portion of conduit I5 indicated by numeral 35. The improved apparatus of the present invention should be located immediately below and extending past the entrance of conduit I4 into the conduit I5.

An apparatus structure in accordance with the description taken with the drawing was installed in a iiuid catalytic cracking unit of the down ow type in the conduit transporting catalyst from the reactor to the regenerator. The catalytic cracking unit was charging hydrocarbon at a feed rate of 25,000 to 30,000 barrels per day. The catalyst circulating in the system had particle diameters in the range from about 0 to 100 mu with the predominating quantity of the catalyst having particle diameters in the range between and 80 mu. Catalyst was circulated through the system at a rate of about 44,000 tons per day. Prior to the installation of the apparatus of the present invention, the pressure drop across the conduit I5 was about 3 pounds per square inch gauge. After the improved apparatus had been installed in the conduit, the pressure drop was lowered to about 0.3 pound per square inch gauge. It will thus be seen that installing the improved apparatus in conduit I5 at a point immediately below cone member 25 where the catalyst flows from conduit I4 to conduit I5 allows a substantial decrease in the pressure drop and resulted in improved circulation of catalyst in the system, and, thus in effect, substantially'l improved the operation in view of the enhanced uidization of the catalyst in the conduit I5.

While the invention has been described and illustrated by reference to the uid catalytic cracking of hydrocarbons, it is to be emphasized that the invention is not restricted to this particular type of operation but may be employed in anyy operation in which finely divided particles drop into a flowing4 stream from a vertical conduit into a transverse conduit. For example, the uidized technique is employed in the synthesis of hydrocarbons from carbon monoxide and hydrogen and it is contemplated that the invention will have application to such -operations. The fluidization of -finely divided particles also has application in chemical manufacture and the present invention may allow improved operations in such reactions by improving the contact of the catalyst with a gaseous medium.

The nature and objects of the present invention having been completely described and illustrated,- what I wish to claim as new and useful and to secure by Letters Patent is:

1. In a catalytic cracking apparatus including a reaction chamber and a regeneration chamber and a conduit connecting said reaction chamber to said regeneration chamber, a vertical conduit from said reaction chamber, a second conduit attached to the lower end of said vertical conduit transverse the vertical conduit and defining a passage from said reaction chamber to said regeneration chamber, a, partition member in said second conduit located at a point below the point of attachment of said Vertical conduit to said second condit, and parallel baiile plates depending from and attached rigidly to said partition member and to the inner walls of said second conduit, said baffle members being arranged in step-like fashion with the downstream end of each baffle member projecting into said second conduit further than the corresponding end of the baffle member above it and each baille member forming an angle less than 180 but greater than with said partition member.

2. In an apparatus for owing a nely divided solid as a suspension in a gaseous medium, a vertical conduit, a second conduit attached to the lower end of said vertical conduit and transverse the vertical conduit, a partition member in said second conduit located at a point below the point of attachment of said vertical conduit and said second conduit, and parallel baille plates depending from and attached rigidly to said partition member and the inner Walls of said second conduit, said baille members being arranged in step-like fashion with the downstream end of each baiile member projecting into said second conduit further than the corresponding end of the baflle member above it and each baille vmember forming an angle less than but greater than 90 with said partition member.

3. In an apparatus for flowing a nely divided solid as a suspension in a gaseous medium, a vertical conduit, a second conduit attached to the lower end of'said vertical conduit and transverse the vertical conduit, a cone shaped member in said vertical conduit adjacent the second conduit attached to said vertical conduit transverse the vertical conduit and defining a passage from said vertical to said second conduit, a partition member in said second conduit located at a point below the point of attachment of said vertical conduit to said second conduit and immediately below said cone shaped member, and parallel baille plates depending from and attached rigidly to said partition member and to the inner walls of said second conduit, said baie members being arranged in step-like fashion with the downstream end of each baille member projecting into said second conduit further than the corresponding end of the baille member above it and each 7 baffle. member formingV an anglev` less than 180',y Number but gxeaterthan 90- with said partitionl member. 2,380,324` JEWELLS. PALMER'.` 2,407,374- 2,416,608 REFERENCES CITED 2,421,212-r The followingk references AareA of recordv in the 111eY of this patent: ,q 1 umbex UNITED STATES PATENTS 141,903 Number Name Date m Cox` Jan; 13,1929

Name Date Munday Ju1y10, 1945' Kollenberg Sept. 10, 19469 Brachenbury- Feb. 25, 1947 Medlin- May 2'7; 1947 FOREIGN PATENTS Country Date Great Brtain1 Apr. 29,1920 

1. IN A CATALYST CRACKING APPARATUS INCLUDING A REACTION CHAMBER AND A REGENERATION CHAMBER AND A CONDUIT CONNECTION SAID REACTION CHAMBER TO SAID REGENERATION CHAMBER, A VERTICAL CONDUIT FROM SAID REACTION CHAMBER, A SECOND CONDUIT ATTACHED TO THE LOWER END OF SAID VERTICAL CONDUIT TRANSVERSE THE VERTICAL CONDUIT AND DEFINING A PASSAGE FROM SAID REACTION CHAMBER TO SAID REGENERATION CHAMBER, A PARTITION MEMBER IN SAID SECOND CONDUIT LOCATED AT A POINT BELOW THE POINT OF ATTACHMENT OF SAID VERTICAL CONDUIT TO SAID SECOND CONDIT, AND PARALLEL BAFFLE PLATES DEPENDING FROM SAID ATTACHED RIGIDLY TO SAID PARTITION MEMBER AND TO THE INNER WALLS OF SAID SECOND CONDUIT, SAID BAFFLE MEMBERS BEING ARRANGED IN STEP-LIKE FASHION WITH THE DOWNSTREAM END OF EACH BAFFLE MEMBER PROJECTING INTO SAID SECOND CONDUIT FURTHER THAN THE CORRESPONDING END OF THE BAFFLE MEMBER ABOVE IT AND EACH BAFFLE MEMBER FORMING AN ANGLE LESS THAN 180* BUT GREATER THAN 90* WITH SAID PARTITION MEMBER. 